JP2017535706A - Methods and equipment for simultaneous generation of mechanical power and production of hydrocarbons - Google Patents

Abstract

A method for combined generation of mechanical power and production of hydrocarbons is proposed, and combustion exhaust gas (c) is generated by igniting at least one internal combustion engine (1) to generate mechanical power And at least one reactor (2) is heated using fuel (e) and combustion assisting gas (d) to produce hydrocarbons. In the present invention, it is provided that at least a portion of the combustion assist gas (d) is heated by indirect heat exchange with at least a portion of the combustion exhaust gas (c) from the internal combustion engine (1). The invention also relates to corresponding equipment (100, 200). [Selection] Figure 4

Description

  The present invention relates to a method and equipment for the simultaneous production of mechanical power and the production of hydrocarbons according to the preamble of the independent claim.

  Some methods of producing chemical reaction products use a reactor with a reaction tube heated by a burner, passing a feed stream through the reaction tube and then at least partially reacting the feed stream. To produce the desired reaction product. Examples of this type of process are steam cracking, alkane dehydrogenation, and even synthesis gas or ammonia production.

  Corresponding methods and apparatus are extensively described in the literature. In the case of the method and apparatus for steam cracking, reference can be made, for example, to Non-Patent Document 1. A method and apparatus for the dehydrogenation of alkanes, in particular from propane to propylene and from isobutane to isobutene, can be found, for example, in Non-Patent Document 2.

  It has long been desired to combine such reactors with devices that generate mechanical power. This can be achieved, for example, by the use of an internal combustion engine, in particular a gas turbine. Known gas / steam methods and corresponding devices serve as an example of this type of combined method.

  In the gas / steam method shown in FIG. 1 and described herein below, an oxygen-containing combustion assist gas, typically air, is drawn into a gas turbine and compressed. A suitable fuel, typically natural gas or some other gas mixture, is introduced into the combustion chamber of the gas turbine and burned under pressure in an atmosphere generated by the combustion assist gas. The decompression of the combustion exhaust gas thus generated (also known as hot gas) drives the expansion stage of the gas turbine, thereby driving the generator coupled to the gas turbine.

  The heat still present in the combustion exhaust gas downstream of the gas turbine can be used in a waste heat steam generator (so-called heat recovery steam generator, HRSG) to generate pressurized steam. Pressurized steam can be used to drive a steam turbine. Steam turbine power is typically used to further generate electrical energy in a generator coupled to a gas turbine, or in another generator.

  The combined process using the gas turbine and heated reactor described hereinabove is basically known as described with reference to FIG. However, as will be described in detail herein below, there is a significant reduction in efficiency in the radiation area of the reactor used in this type of instrument. Thus, the overall efficiency of such equipment is, at best, only slightly higher than the efficiency of individual devices that produce electrical energy and recover hydrocarbons. Thus, the advantages over low efficiency composite devices usually do not justify the cost of combining them.

  In particular, in this type of apparatus, the operation of the heated reactor depends on the operation of the gas turbine. If the gas turbine becomes unusable, in extreme cases the reactor must also be shut off, thus resulting in a loss of manufacturing costs. Typically, the reactor described above may be designed for long-term operation over several years, or is configured in the form of several parallel units that are serviced or regenerated alternately. In the steam cracking method, for example, 5 to 10 reactors may be operating at all times, one in the so-called decoking mode. However, gas turbines require significantly more frequent maintenance.

  Patent document 1 is disclosing the power plant which has a high-speed fluidized bed reactor. A subdivided heat transfer fluidized bed is provided, which is designated to swirl the hot ash produced by the fluidized bed reactor and extract heat from the ash. Means are provided to control the portion of the hot ash that circulates through the sections of the heat transfer bed formed by subdivision so as to control the power gain of each section. One section of the subdivided fluidized bed can produce process steam and the other section can supply hot process air to the turbine.

  From Patent Document 2 and Patent Document 3, a combined method of performing autothermal reforming and operating a turbine is known. From Patent Document 4, a reforming reactor that is operated in combination with a turbine is known.

GB2147734A US 5,048,284A GB2296719A FR1445870A

Paper "Ethylene", Ullmann's Encyclopedia of Industrial Chemistry, Online, April 15, 2007, DOI 10.1002 / 143356007. a10_045. pub2 The paper “Propene”, Ullmann's Encyclopedia of Industrial Chemistry, Online Edition, June 15, 2000, DOI 10.1002 / 143560007. a22_2111, section4.3. , "Propane Dehydration"

  The object of the present invention is therefore to improve the combined process for the production of electrical energy and the production of hydrocarbons, in particular in terms of efficiency.

  This problem is solved by a method and apparatus for mechanical power generation and hydrocarbon production having the features of the independent claims. Preferred embodiments are the subject matter of the dependent claims and are described below.

  Before describing the features of the present invention, the basics of the present invention and terms used will be described.

  In the following description, reference will be made frequently to the efficiency of heat treatment, but the following definitions apply.

Technical combustion ("heat") efficiency (FTW, ny_FTW) indicates the fraction of the induction heating power (P_supply) that is not lost to the environment through the combustion exhaust gas (P_exhaust gas):
ny_FTW = 1-P_exhaust gas / P_supply

  The loss to the environment caused by the heat conduction of the high temperature components is not taken into account here as this loss is typically significantly less than the exhaust gas loss.

Radiation zone efficiency (SZW, ny_SZ) indicates the fraction of induction heating power (P_supply) that is indirectly transmitted to the processing medium (P_treatment) in the ignition chamber:
ny_SZ = P_processing / P_supply

  Transmission is typically caused by radiation, preferably at temperatures significantly above 1,000 ° C. Although the reactor is heated only directly, ie, only by the burner, for example, not by preheated combustion air, the typical radiant zone efficiency of this reactor is about 0.42 (42 %).

The electric efficiency (ny_el) indicates the ratio of the heating input power (P_supply) of the heat output method that is released as a net output in the form of electric power (net output is the output of the heat output method, pump and compressor Etc. shows the output with reduced power required for auxiliary equipment):
ny_el = P_el / P_supply

  The term “energy efficiency” is generally used herein as a comparative term, and it is a different method or compound to produce a specific amount of one or more products or to generate a specific power. Assess or quantify the heating power required for the method. The term is used for power generation by, for example, a single stage steam method, a gas turbine and a combined gas / steam method. Typically, the efficiency increases in the order specified, i.e., the heating power used for the specific amount of current produced decreases.

  Fuel ignition output is typically related to lower heating or heating value (Hu) within the scope of this application. Ignition output refers to the maximum amount of heat based on the amount of fuel used that can be used in combustion where condensation of water vapor is not contained in the exhaust gas.

  In general terms, the term “gas turbine”, as already mentioned, comprises a compression stage as an actual gas turbine, an expansion stage, and a combustion chamber connected between the compression stage and the expansion stage. Point to. The combustion chamber supplies compressed combustion support gas such as air through the compression stage. Fuel (generally liquid or gaseous) enters the combustion chamber through the fuel inlet. The fuel burns with the gas mixture in the combustion chamber to produce combustion exhaust gas, so-called hot gas.

  The hot gas is depressurized in the expansion stage, at which point the heat output is converted to mechanical power. Mechanical power is reduced by one or more shafts. Some of the mechanical power is used to operate the compression stage while the rest is used, for example, to drive a generator. After decompression, the combustion gas is discharged as exhaust gas or used as a heating medium, as in the case of the present invention.

  Within the scope of this application, the term “combustion assisting gas” does not necessarily mean that the combustion of the fuel occurs with air (“combustion air”), but a different gas mixture (this gas mixture must contain oxygen). Is used to express the notion that it can occur among others.

  As in the case of gas turbines, the ignition reactor described above in this specification is fed with combustion support gas in addition to fuel, which combustion support gas is contained in a corresponding burner for underburning. Burn. Typically, air is used as a combustion assist gas. However, it is also possible to at least partly use the combustion exhaust gas from the gas turbine as the combustion support gas. This is possible because the combustion of fuel in a gas turbine typically occurs with a significant superstoichiometric oxygen supply. Thus, a substantial amount of oxygen is still present in the combustion exhaust gas, allowing the combustion exhaust gas to be used in the reactor as a combustion assist gas. In addition to the combustion exhaust gases from the gas turbine, additional air or oxygen-containing gas mixtures can be used in such reactors to regulate combustion. The problems that arise when using the combustion exhaust gas from a gas turbine as a combustion assist gas are described below and form the starting point of the present invention.

  The invention starts from a method known in principle for the combined production of mechanical power and the production of hydrocarbons, which ignites and burns at least one internal combustion engine to produce mechanical power. At least one reactor is heated using fuel and combustion assist gas to produce exhaust gases and hydrocarbons.

  In accordance with the present invention, it is provided that at least a portion of the combustion assist gas is heated by indirect heat exchange with at least a portion of the combustion exhaust gas from the internal combustion engine. In other words, according to the present invention, not all of the combustion exhaust gas is supplied to the reactor, but a portion of the combustion exhaust gas is supplied. Combustion assist gas, for example air, supplied from the outside is preheated by a part or all of the combustion exhaust gas.

  Where this application refers to “feeding” or “feeding” fuel, combustion assist gas and / or combustion exhaust gas into the reactor, this corresponds rather than in the reaction zone, eg in the reactor reaction tube. It means feeding them into a burner or a combustion chamber. A gas mixture passing through a reaction zone, for example a reaction tube, is referred to as process gas (tube side) within the scope of the present application.

  The invention is particularly suitable for a method of driving a generator using at least partly the generated mechanical power, i.e. converting the mechanical power at least partly into electric power. However, the invention can also be used to advantage, for example, when at least one shaft of the compressor and / or pump is driven at least partly by mechanical power. In this case, the drive unit may be part of the method used for the production of hydrocarbons, for example. For example, mechanical power can be used to drive a compressor that compresses the process gas or vapor.

  The invention relates to the efficiency in the corresponding combined process according to the prior art, more precisely the radiation zone efficiency in the reactor as defined herein above, in particular in terms of energy balance, in the reactor. Based on the finding that a significant percentage of the combustion exhaust gas energy from gas turbines that feed directly and support fuel combustion is significantly reduced by the fact that they are already removed in the gas turbine . Specifically, this can be indicated by the oxygen content of the corresponding combustion exhaust gas.

  Inevitably, even if combustion occurs in the gas turbine with significant superstoichiometric oxygen supply, the oxygen content of the combustion assist gas is reduced in the gas turbine. As usual, when air having a natural oxygen content of about 21% is used as a combustion assist gas in a gas turbine, this oxygen content drops to about 14% in the combustion exhaust gas.

  However, in corresponding reactors, particularly those used for steam cracking, the radiation zone efficiency is essentially dependent on the temperature obtained by the combustion of the fuel and can be transmitted through the reaction tube to the feed stream. . In a conventional process, ie, a self-operating reactor that is not coupled to a gas turbine, the adiabatic combustion temperature reaches about 2,000 ° C. when air is used as the combustion assist gas. The adiabatic combustion temperature is the temperature that the gas mixture will obtain after combustion is complete when there is no heat exchange with the environment during combustion. This is therefore a theoretical temperature that is not actually achieved because such a reactor does not actually operate adiabatically. However, adiabatic combustion temperature is a comparative term used in the art and most conveniently represents a variable on which the radiation area efficiency depends.

  If the combustion assist gas contains less oxygen due to partial reaction of oxygen in the upstream gas turbine, only an adiabatic temperature of about 1750 ° C. can be achieved. Combustion exhaust leaves the gas turbine at, for example, about 600 ° C., so that the adiabatic combustion temperature of a conventional reactor is reached due to the reduced oxygen content, despite the considerable amount of heat available. It is no longer enough.

  Under simple conditions (again from the point of view of energy balance), the gas turbine exhausts about one third of the heat output supplied to the gas turbine as shaft power, and the heat output supplied by the gas turbine. However, assuming that about one third of the heat output supplied to the gas turbine and reactor as a whole constitutes one ninth of the total heat output is removed from the combustion exhaust gas in the form of shaft power. Accordingly, in response, the adiabatic combustion temperature is reduced by about a factor of nine.

  Thus, as already explained, the present invention should not be used to feed all combustion exhaust gas into the reactor and assist in the combustion of fuel, but at best uses a portion of the combustion exhaust gas. It suggests what should be done. Thus, in contrast to conventional coupling equipment configurations, a partial or dedicated external combustion assist gas, such as fresh combustion air, that is not generated from the combustion exhaust gas is supplied to the reactor. The actual coupling between the gas turbine and the corresponding reactor is performed by a preheating device, which comprises, for example, one or more suitable heat exchangers for indirect heat exchange. Because of the indirect heat exchange between the combustion exhaust gas and the combustion support gas, its temperature is certainly utilized (ie, it transfers heat output), but the oxygen content of the combustion support gas is not affected. In this way, for example, fresh air containing about 21% oxygen can be heated as a combustion assist gas and fed into the reactor. Therefore, once again the adiabatic combustion temperature of about 2,000 ° C. already described (when part of the combustion exhaust gas is used only for preheating and part of the combustion exhaust gas is fed into the reactor), or Higher temperatures (when used exclusively for preheating) can be achieved as described herein below.

  As described above, on the one hand, the combustion exhaust gas is partially used only for preheating, and on the other hand, the combustion exhaust gas is partially fed into the reactor, for example, a portion of the combustion exhaust gas and “fresh” "Mixing with a combustion assisting gas, such as air, thereby achieving a predetermined oxygen content. For example, an oxygen content of about 19% can be selected. Another portion of the combustion exhaust gas is not fed into the reactor but is used only for preheating the combustion assist gas by indirect heat exchange. Assuming a combustion exhaust gas temperature of about 600 ° C., the adiabatic combustion temperature of about 2,000 ° C. described above can be achieved in the reactor, and thus the radiation zone efficiency is the efficiency obtained in a conventional reactor. Can be achieved equally. Therefore, the operation of the reactor may be negligible, even if it is adjusted.

  Another essential advantage of the present invention is that the reactor can continue to operate even when the gas turbine is unusable or needs service. In this case, air that has not been preheated can be used, for example, as combustion assist gas. Alternatively, in this case, the combustion support gas can be preheated in some other way, for example using steam and / or flue gas. Accordingly, the corresponding preheating equipment need only be designed for short-term operation and is accordingly inexpensive.

  In this regard, in the conventional apparatus such as the apparatus shown in FIG. 3, in addition to the combustion exhaust gas, further combustion support gas can be supplied from the gas turbine, and all of the combustion exhaust gas and the combustion support gas can be supplied. Should be fed to the reactor. However, this has traditionally been done only to adjust for variability and to achieve increased independence between the gas turbine and the reactor. The problems of reduced oxygen content in the reactor and reduced radiation zone efficiency are not inherently solved by this method.

  Within the scope of the present invention, in contrast, the radiation area efficiency of the reactor can be significantly increased. The reactor can operate at a radiation zone efficiency level, which can also be achieved in a self-supporting reactor as described hereinabove. However, it is also possible to further increase the radiation area efficiency by preheating and achieving higher temperatures in the reactor.

  The following summarizes embodiments of the invention as defined in the claims and partially described above in this specification.

  In particular, the method of the present invention is suitable for use in the tubular reactors described hereinabove, i.e. in an apparatus in which at least one reactor is realized as a tubular reactor. In the radiation zone, the reaction tube is externally heated by a burner that burns fuel. Conventional reactors that operate in a self-supporting manner include a feed opening through which combustion support gas is fed. Inside the reactor or the corresponding reactor combustion chamber, there is a slight negative pressure generated by the blower in the flue gas passage. Accordingly, the combustion support gas is automatically taken in. In contrast, the present invention involves delivering combustion support gas into the corresponding reactor or its combustion chamber by a blower under slight positive pressure. Such a feeding method is typical for preheating air, for example, in a hydrogen reforming method.

  The process according to the present invention is a steam-cracking process as described hereinabove, ie a hydrocarbon-containing feed stream through the reaction tube of a reactor configured as a tubular reactor to produce (olefin) hydrocarbons. Particularly suitable for the method of feeding steam to steam. In a corresponding steam cracking method, the above mentioned temperature spreads within the radiation zone. However, the present invention relates to a catalytic method, for example, a method for dehydrogenation of alkane as described above, that is, a method comprising a reactor, in which a catalyst is provided in a reaction tube, or a hydrogen reforming method. Is equally suitable.

  As already mentioned, the process according to the invention is particularly advantageous because it allows the temperatures that can be achieved thereby to reach a high radiation zone efficiency for the reactor. This in turn means that the method heats at least one region of the at least one reactor to an adiabatic combustion temperature, typically 1500-2500 ° C., through the use of fuel and combustion assist gas. Means to be used in case.

  A suitable internal combustion engine for use with the present invention is specifically a gas turbine. This is because gas turbines have good mechanical or electrical efficiency while having high nominal power at a relatively low cost. Thus, gas turbines are typically used in power plants. Also, the mechanical efficiency of the gas turbine alone is typically less than that of the correspondingly configured diesel engine or coal / steam power plant. This type of internal combustion engine is also suitable for use in the present invention because the temperature of the combustion exhaust gas is about 600 ° C. for a diesel engine and about 700-1,000 ° C. for a gasoline engine.

  While one conventional drawback of using gas turbines is the use of relatively high quality fuel (gas), this is actually an advantage in the present invention. In the process described here (for example in steam cracking processes and hydrogen reforming), the reaction product is produced, so-called waste gas having a high value in terms of combustion is obtained as residual gas. This residual gas is a methane-containing fraction or a mixture of carbon monoxide, carbon dioxide and hydrogen (synthesis gas). Accordingly, the (partial) method of producing reaction products, performed within the scope of the present invention, provides a suitable fuel for the gas turbine. Needless to say, the corresponding gas mixture can also be combusted in the engine. This results in a further synergistic integration of the corresponding parts of the device.

  When the exhaust gas from the internal combustion engine is supplied at a temperature level of less than 650 ° C. as in this case, it is particularly advantageous because the combustion support gas can be heated particularly effectively and inexpensively. For example, the material costs of using heat exchangers are still significantly lower at such temperatures. However, in general, the combustion exhaust gas from an internal combustion engine can be supplied at a temperature level of 500-1000 ° C, in particular at a temperature level of 600-700 ° C, or a temperature level of 500-650 ° C.

  In a method according to an embodiment of the invention, advantageously, a portion of the exhaust gas from the internal combustion engine is used to heat the combustion assist gas by indirect heat exchange, and a portion of the combustion from the internal combustion engine is performed. The exhaust gas is mixed with the combustion support gas and supplied to the at least one reactor together with the combustion support gas. The exhaust gas is partly used for preheating and partly used to feed into the reactor, thereby allowing a particularly favorable combustion of the gas turbine or another internal combustion engine and reactor. In this case, the conditions in the reactor can be approximated to those of a conventional free-standing reactor, which must be changed to the operating mode of the corresponding reactor and / or their construction configuration. It means that there is little or no need to change. Reaction tubes and equipment that use waste heat (in so-called convection zones) can be retained.

  However, in the new facility configuration, the exhaust gas from the internal combustion engine is completely used to heat the combustion support gas by indirect heat exchange and not to supply the combustion support gas to at least one reactor. Can prove to be advantageous. Thus, at least one reactor receives the total oxygen content of the combustion assist gas, eg air, in addition to the heat of the exhaust gas, so that the temperature of such a reactor can be further increased. In this way, the radiation zone efficiency of the corresponding reactor is considerably increased. Fuel consumption in the reactor can be reduced accordingly by the present method.

  The invention is particularly suitable for use with air as fuel, natural gas, methane-containing gas mixtures and / or synthesis gas, and / or combustion support gas. As already mentioned, the corresponding fuel is a typical residual gas from the corresponding method of producing the reaction product (eg from a method for steam cracking, synthesis gas generation, or hydrogen reforming). Also good. The invention in particular allows fuel savings by increasing efficiency.

  A further advantage of the method according to the invention is obtained when pressurized steam is generated from waste heat from at least one reactor and used to drive at least one shaft, in particular the generator shaft. In this way, additional mechanical power can be obtained and used beneficially even when the corresponding pressurized steam is at a lower pressure. The steam obtained from waste heat from at least one reactor is basically only by-products that can beneficially use heat (waste heat) that cannot be used in the reaction. In a theoretical ideal case, only the heat of reaction is generated in the reactor and no waste heat, i.e. steam, is generated.

  An advantage of the present invention is that the amount of pressurized steam produced by waste heat from one or more reactors can be minimized. Pressurized steam produced by waste heat from one or more reactors is significantly higher than the steam method of a power plant (a multi-stage method that is more efficient at its peak at higher pressures / temperatures). Obtained with ghee loss. Pressurized steam can be used with nearly 100% efficiency, for example, as partially heated steam that preheats one or more feed streams in a steam cracking process. In the case of generating mechanical power in the turbine, the efficiency is about one-half worse than that in the steam method.

  See in particular the above comments regarding the features and advantages of the apparatus for mechanical power generation and hydrocarbon production provided by the present invention and specifically configured to carry out the methods described hereinabove. I want to be.

  The invention and specific embodiments of the invention are illustrated by the accompanying drawings in comparison with the prior art.

1 is a simplified schematic diagram of a gas and steam power plant according to the prior art. 1 is a simplified schematic diagram of an ignition reactor operating in accordance with the prior art. 1 is a simplified schematic diagram of a device having a gas turbine and an ignition reactor according to the prior art; FIG. 1 is a simplified schematic diagram of an apparatus having a gas turbine and an ignition reactor according to an embodiment of the present invention. 1 is a simplified schematic diagram of an apparatus having a gas turbine and an ignition reactor according to an embodiment of the present invention.

  In the drawings, corresponding elements are designated with the same reference numerals and the description will not be repeated for clarity. The same applies to fluid flow, even if the fluid flow shown in lower case is supplied in different amounts, as will be explained below.

  In all illustrated embodiments, when a reactor is illustrated, the reactor is arranged to perform a steam cracking process, i.e., the reactor is fed with a hydrocarbon-containing feed stream that mixes with the steam. To do. The fuel used is the appropriate combustion gas described above, while air is used as the combustion support gas. However, the illustrated apparatus is theoretically also suitable for performing other methods of producing reaction products or using other fuels and combustion assist gases. Although the following description frequently refers to “one” reactor or “one” gas turbine, the corresponding equipment configuration may also include several reactors or gas turbines.

  FIG. 1 shows a simplified schematic diagram of a prior art gas and steam power plant, designated as 300 as a whole.

  The gas and steam power plant 300 includes a gas turbine 1 as a central component, and the gas turbine 1 includes a compression stage 11 and an expansion stage 12, and a compression stage 11 as described above in this specification. Although provided with a combustion chamber disposed between the expansion stage 12, the combustion chamber is not shown separately herein. The generator G is driven by the gas turbine 1. The gas turbine 1 supplies a combustion support gas a that is compressed in the compression stage 11. The fuel b is supplied to a combustion chamber (not shown) of the gas turbine 1 and burned in an atmosphere generated by the combustion support gas a under the pressure of the combustion chamber.

  Combustion typically occurs at a lambda value of, for example, about 3 with significant superstoichiometric oxygen supply, and a combustion exhaust gas produced during combustion that can be expanded in the expansion stage 12 of the gas turbine. c (hot gas) still has a substantial oxygen content. When air having a natural oxygen content of about 21% is used as the combustion support gas a, the combustion exhaust gas c still has an oxygen content of about 14%.

  For example, the combustion exhaust gas c that can be set to a temperature of 600 ° C. is supplied to the heat recovery steam generator 5 in the gas / steam power plant 300. Typically, a small amount of further fuel is supplied to the heat recovery steam generator 5, that is, the heat recovery steam generator 5 mainly uses the sensible heat of the combustion exhaust gas c. The combustion exhaust gas g cooled accordingly is discharged from the heat recovery steam generator 5.

  In the fairly simple view of FIG. 1, pressurized steam f is generated. Typically, the corresponding gas and steam power plant 300 produces pressurized steam f at three pressure levels. The pressure levels are, for example, about 130, 30 and 8 bar, and steam is partially removed from the turbine at moderate pressure levels (by “tapping”), medium pressure levels, and low pressure levels, and moderate The steam at a pressure level of 1 starts at about 570 ° C. starting from the saturated steam temperature (“intermediate superheat”). The purpose of this procedure is to minimize exergy loss by transferring heat from the combustion exhaust gas c to the feed water or steam with the smallest possible temperature difference.

  The pressurized steam f is used in the decompression turbine 6 (steam turbine) and generates shaft power (mechanical power). Next, this power is converted into electric power by the generator G. This generator may be the same as the generator G coupled to the gas turbine 1 or may be provided separately. The reduced-pressure steam flow (not specified in FIG. 1) is cooled by the cooler 7 using, for example, cooling water. The resulting vapor condensate is reused in the process (using a so-called boiler feed pump).

Typical characteristic values of the gas / power plant 300 are shown below. The corresponding variable is shown for a net power of 100 MW. This is because the power of 100 MW is necessary for the size of the steam cracking equipment corresponding to the prior art. In the field of power plants, a net power of 80-400 MW per gas turbine unit is typical. Standard 619,000 cubic meters per hour (Nm ³ / h) of fuel air is used as the combustion support gas a, and the lower output of fuel b is about 180 MW. Corresponding values are summarized in the table below. Any rounding error is ignored.

In the case shown, typically a combustion exhaust gas c of about 640,000 Nm ³ / h is produced. The amount of cooled combustion exhaust gas g in this case is also about 640,000 Nm ³ / h in the absence of further ignition in the heat recovery steam generator 5.

  Typically, the electrical efficiency of the gas turbine 1 and the electrical efficiency of the generator connected to the gas turbine 1 is about 0.36 (36%). The electrical efficiency of the vacuum turbine 6 is about 0.32 based on the energy supplied to the heat recovery steam generator 5, or about 0.20 based on the total energy used. The proportion of the total power of the corresponding gas / steam power plant constituted by the decompression turbine 6 is also about 0.36 in the illustrated embodiment, for example. The thermal efficiency that does not take into account the cooler 7 is about 0.82 in the embodiment. (The thermal efficiency varies depending on the condensation temperature, the amount of steam, etc., and varies within a range from about 0.75 to about 0.85.) Thermal efficiency is often not particularly significant in the case of the present invention. . This is because even if most of the heat is taken from flue gas, for example, simply supplying hot water or high temperature steam, if these cannot be used with high efficiency, the efficiency of the corresponding equipment will be reduced. This is because it does not increase almost.

  Of this, about 64 MW of the lower output of about 180 MW of the fuel b in the generator G coupled to the gas turbine 1 is obtained as electric power, and about 112 MW is the combustion exhaust gas c as sensible heat. The heat loss typically corresponds to about 3 MW. Next, of the approximately 112 MW perceptible heat in the combustion exhaust gas c, typically about 3 MW remains in the cooled combustion exhaust gas g, which is cooled to a temperature of about 128 ° C. To do. Of the remaining approximately 80 MW, 36 MW is obtained as power in the generator G coupled to the decompression turbine 6, and approximately 44 MW is discharged in the cooler 7.

  Using a total heating power of about 180 MW and power of about 100 MW for the two generators G, the total electrical efficiency of the gas and steam power plant 300 is about 0.56 in an embodiment. In trial operation, efficiencies up to 0.61 have been achieved in large gas and steam power plants (in the case of about 800 MW output), but this efficiency drops significantly as the cooling water gets warmer.

  FIG. 2 shows a simplified schematic diagram of a prior art ignition reactor, designated as 2 as a whole. As already explained, this type of ignition reactor can typically be used to produce hydrocarbons or synthesis gas, for example by steam cracking. Corresponding reactors 2 typically comprise a radiation zone 21 and a convection zone 22 as is generally known. In the radiation area 21, several burners (not shown) that supply fuel d are typically arranged. Combustion is enabled by supplying the combustion support gas e. In the radiation zone 21 and the convection zone 22 there are typically reaction tubes heated from the outside by corresponding burners.

  Similarly, the ignition reactor 2 uses most of the waste heat for the generation of the pressurized steam f, but the pressurized steam f is typically used with a sufficient generation efficiency of electric energy. Is relatively unsuitable. The less useful value of pressurized steam f from the typical ignition reactor 2 shown in FIG. 2 is that the temperature is relatively low and the pressure is relatively low, and only one steam level is achieved (thus, This is due to the fact that exergy loss is relatively large during steam power generation). In a typical gas / steam power plant, for example, the gas / steam power plant 300 shown in FIG. 1, the pressurized steam f is obtained at 130 bar and 570 ° C., but it is heated from the ignition reactor 2 shown in FIG. The pressure of the pressurized steam f is typically only 120 bar and its temperature is typically only 520 ° C. Typically, the corresponding pressurized steam f from the ignition reactor 2 is used to recover shaft power (eg, in a steam cracking device) and use it as heated steam. Here too, the cooled combustion exhaust gas g is obtained.

In corresponding energy balance considerations, assuming a lower power of about 1,000 MW in the form of fuel d (typically distributed across several reactors), for example about 1,067,000 Nm ³ / h of combustion air as combustion support gas e is fed into the radiation zone 21 with a typical radiation zone efficiency of about 0.42, which is a typical value for a reactor used in a steam cracking process. Assuming that about 512 MW or about 595 t / h of pressurized steam f can be obtained from the waste heat from the reactor 2. About 60 MW enters the cooling flue gas g, which is removed in an amount of about 1,172,000 Nm ³ / h and a temperature of about 128 ° C. The “disappeared” 428 MW heating power is exhausted in the form of chemical binding energy and sensible heat in the tube side process gas, ie, from the reaction zone of the reactor 2 rather than the flue gas stream. This value is the same for all reactors 2 in the following figures provided as examples herein, since the same amount of reaction product is produced.

  FIG. 3 is a simplified schematic diagram of a combined facility having a gas turbine 1 and an ignition reactor 2 according to the prior art, designated generally as 400. The basic concept of providing such a facility 400 is that the sensible heat of the combustion exhaust gas c from the gas turbine 1 is converted to the corresponding combustion, as in the gas / steam power plant, for example, the gas / steam power plant 300 shown in FIG. It is to be used in the reactor 2. This takes advantage of the above-mentioned fact that the combustion exhaust gas c still has a substantial oxygen content as a result of significant superstoichiometric combustion in the gas turbine 1. Nevertheless, in the illustrated embodiment, a further combustion support gas d, for example air, is fed into the combustion exhaust gas c by means of a blower 3, for example.

  This further supply serves to provide further adjustment variables for adjusting the combustion in the reactor 2.

  However, a significant disadvantage of this type of combined equipment 400 according to the prior art is that the radiation zone efficiency in the radiation zone 21 in the ignition reactor 2 is significantly reduced. Compared to, for example, the self-sustained reactor 2 shown in FIG. 2, the radiation zone efficiency is reduced, for example, from about 0.42 to about 0.37. This is particularly true, even though the combustion exhaust gas c has a relatively high temperature of, for example, about 600 ° C., an oxygen content of, for example, about 14% of the combustion exhaust gas c is still typically used. This can be attributed to the fact that the oxygen content of combustion assisting gases such as combustion air is significantly below. This cannot be compensated for by further supply of combustion air d or a corresponding supply of combustion assisting gas (at least unless very expensive oxygen enrichment is used). When air containing about 21% oxygen is used as a combustion assisting gas d in the reactor 2 operating in a self-supporting manner, shown in FIG. An adiabatic combustion temperature of 000 ° C. can still be achieved. In contrast, in the installation 400 shown in FIG. 3, the adiabatic combustion temperature within the radiation zone 21 is limited to about 1,750 ° C. due to the situation described above. This directly reflects the efficiency of the poorer radiation area described above.

  In terms of energy balance, a substantial proportion of the chemical energy contained in the combustion support gas a is removed in the gas turbine 1 and can therefore no longer be used in the combustion exhaust gas c thereafter. .

Next, at a power of 1,000 MW, one or more reactions for steam cracking operation using the gas turbine power at its maximum, i.e. using the additional combustion exhaust gas d for adjustment at a minimum. Provides exemplary data upstream of the gas turbine of the vessel. For example, when combustion air of about 1,132,000 Nm ³ / h is used as a combustion support gas a in this type of equipment 400, and when a lower output of about 340 MW is used in the form of fuel b, about 118 MW Electric power can be obtained at the efficiency levels already described in the generator G coupled to the gas turbine 1. About 224 MW passes through the combustion exhaust gas c as sensible heat. In particular, the generator G, auxiliary equipment, and gas turbine oil coolers suffer about 5 MW of loss. The combustion exhaust gas c is generated in an amount of about 1,170,000 Nm ³ / h.

In the illustrated embodiment, for example, about 189,000 Nm ³ / h of fuel air is used as the combustion support gas d. The lower output of fuel e is about 922 MW. Thus, the total heating power in the form of the fuels b and e used reaches about 1,270 MW, and the heating power from the sensible heat of the combustion exhaust gas c available in the radiation zone 21 and under the form of the fuel e The heating output from the soot output is about 1,147 MW. Of this, about 650 MW is recovered in the form of pressurized steam f in an amount of about 756 t / h, about 69 MW enters the cooling flue gas g, and the cooling flue gas g is about 128 as described above. Removed at ° C. Therefore, the amount of cooling flue gas g is about 1,457,000 Nm ³ / h compared to about 1,172,000 Nm ³ / h of the above-mentioned self-operating reactor 2 shown in FIG. Again, 428 MW is discharged into the tube-side process gas as chemical binding energy and sensible heat. This is because the same amount of reaction product is produced in the tube-side process gas as in the case of the reactor 2 according to FIG.

  As already mentioned, the radiation area efficiency of the radiation area 21 is reduced to about 0.37. The efficiency level of steam power generation (from pressurized steam f) is about 0.51, and the overall thermal efficiency is about 0.94. (Some of the heat entering the process gas in the radiation zone 21 is used for steam power generation. Therefore, the two efficiency levels should not be added together or supplemented with each other to give a specific thermal efficiency. The amount of heat and chemical bond energy discharged by the process gas is out of the total energy balance, but these values are the same for all reactors 2 shown in the accompanying drawings.

  FIG. 4 shows, in a simplified schematic diagram, a combined apparatus having a gas turbine 1 and an ignition reactor 2 according to an embodiment of the present invention, the apparatus being designated as 100 in its entirety.

  The main aspect of the present invention that has already been described several times is the use of the preheating unit 4, which preheats the combustion support gas b supplied into the reactor 2. In the embodiment shown in FIG. 4, all the combustion exhaust gas c from the gas turbine 1 passes through the preheating unit 4, but it is also possible to use only a part of the combustion exhaust gas c. The preheating unit 4 is shown in FIG. For example, the sensible heat of the combustion exhaust gas C can be transferred to the combustion support gas d by means of a preheating unit 4 which can comprise one or more appropriately configured heat exchangers.

  This has the special advantage that the combustion support gas d such as combustion air, which still has a high oxygen content, can be fed into the reactor 2, but at the same time the combustion support gas d can be heated with the sensible heat of the combustion exhaust gas c. Have. Surprisingly, this is not only in comparison with the reactor of the corresponding coupling facility 400 shown in FIG. 3, but also in the radiation zone 21 of the reactor 2 in comparison with the self-operating reactor 2 shown in FIG. Has been found to substantially increase the radiation area efficiency. As a rule of thumb, preheating at 10 ° C. results in a 0.2% increase in radiation area efficiency.

In the apparatus 100 shown in FIG. 4, a radiation zone efficiency level of about 0.47 is obtained in the radiation zone. When combustion air of about 383,000 Nm ³ / h is used as combustion support gas a and a lower output of about 108 MW is used in the form of flow b, about 40 MW of power is generated by gas turbine 1 or corresponding generator G. Can be obtained. The combustion exhaust gas c is about 656 ° C. (this is an example value, typical values are 550-700 ° C.), corresponding to a sensible heat of about 76 MW. Next, downstream of the preheating unit 4, the temperature of the combustion exhaust gas c is still 105 ° C., corresponding to sensible heat of about 10 MW.

  The temperature of the cooled combustion exhaust gas (flue gas temperature) is typically determined by the so-called “sulfur dew point”. At this temperature, aqueous sulfuric acid is concentrated and severe corrosion occurs. The sulfur dew point is significantly lower at a lambda value of 3 (such as gas turbine flue gas) than at a lambda value of 1.1 (in the steam cracking reactor). This is because, in proportion, there is a smaller amount (typically sulfur-containing) fuel or combustion product. An exemplary value for a typical heated gas is 105 ° C. on the one hand and 128 ° C. on the other hand.

The amount of combustion exhaust gas c is about 395,000 Nm ³ / h. In addition to this, combustion air of about 879,000 Nm ³ / h is supplied as a combustion support gas in the form of steam d, for example, at about 28 ° C., and this combustion air is heated to 286 ° C. in the preheating unit 4 (about If the lower power of the fuel e form is about 824 MW, the total heating power available is about 942 MW, and the heating power available in the reactor 2 is about 890 MW. is there. Of these about 890 MW, the remainder of about 462 MW is produced with a radiation zone efficiency of about 0.47, of which about 408 MW is obtained in the form of pressurized steam f at about 475 t / h and about 54 MW is At about 128 ° C. or about 966,000 Nm ³ / h in the form of cooled flue gas g.

  In the corresponding device 100, the combustion assisting gas d can be preheated to significantly higher temperatures (see below), as illustrated in the table only.

  FIG. 5 shows, in a simplified schematic diagram, a combined device having a gas turbine 1 and an ignition reactor 2 according to another embodiment of the present invention, the device being designated as 200 in its entirety. The apparatus 200 differs from the apparatus 100 shown in FIG. 4 in that only a part of the combustion exhaust gas c flow passes through the preheating unit 4. This partial flow is designated as c ′ in the apparatus 200. Another partial flow, designated herein as c ″, is combined with the combustion support gas d. This provides a particularly flexible operation for the facility 200 or, as explained, the operating conditions of the reactor 2 can be approximated to the operating conditions of the self-sustaining reactor 2 shown in FIG.

  Corresponding embodiment or installation 200 of the invention according to FIG. 5 may in particular comprise supplying the partial flows c ′ and c ″ in adjustable amounts, and providing a heat supply of combustion exhaust gas c and / or It can be adapted to each thermal requirement in the reactor 2. Similarly, examples of characteristic values of the facility 200 are shown below.

When combustion air is supplied into the facility 200 as a combustion support gas a in an amount of about 1,035,000 Nm ³ / h and the lower power output in the form of fuel d of about 318 MW is used, about 107.8 MW of power is consumed. The gas turbine 1 can produce an efficiency level of about 0.34. The electrical efficiency of the corresponding installation is somewhat lower than that of a simple power plant gas turbine (see description associated with FIG. 1; efficiency level in FIG. 1 is 0.36). This is because it is further necessary to overcome the pressure loss through the reactor 2.

In the entire combustion exhaust gas c, sensible heat remains, which corresponds to about 211 MW. When a partial flow c ′ corresponding to a heat quantity of about 77 MW is supplied, sensible heat corresponding to about 67 MW can be transferred to the combustion air by this partial flow c ′, which in this case is a combustion assist The gas d is used in the preheating unit 4. Downstream of the preheating unit 4, about 10 MW of sensible heat remains in the partial stream c ′, which is supplied in an amount of about 391,000 Nm ³ / h, which is about 656 ° C. to 105 ° C. (See the description for FIG. 4 for the subject of sulfur dew point).

As already described, the combustion air is supplied, for example, by the blower 3 at a temperature of about 28 ° C. (eg, ambient temperature) as the combustion support gas d. The amount of combustion air is, for example, about 397,000 Nm ³ / h. In the preheating unit 4, the combustion air is heated to about 627 ° C., which corresponds to about 67 MW of stream c ′. The partial flow c ″ of the combustion exhaust gas c is supplied in an amount of about 679,000 Nm ³ / h, which corresponds to a sensible heat of about 134 MW. Further, a fuel e corresponding to about 799 MW is supplied to the reactor 2.

Accordingly, a total heating power of about 1,000 MW is available in the reactor 2 and a total heating power of about 1,118 MW is available in the facility 200 as a whole. By appropriately adjusting the partial flows c ′ and c ″, a radiation zone efficiency of about 0.42 can be achieved in the radiation zone 21 of the reactor 2, which is the self-sustaining reaction shown in FIG. This corresponds exactly to the efficiency of the vessel 2. 512 MW remains in the pressurized steam f supplied at about 595 t / h, and about 60 MW remains in the cooled combustion exhaust gas c, of which about 1,172,000 Nm ³ / h is supplied at 128 ° C.

  In the following Tables 1 to 5, the flow rate and energy content already described with respect to FIGS. 1 to 5 are shown again, and for the installation 100 shown in FIG. 4 or FIG. 4, Tables 4A and 4B show two operating cases: When the combustion support gas d is preheated to 286 ° C. (when conventional process control can be performed in the reactor 2; see above), and when preheated to 498 ° C. (partial overheating only or outside the feed stream / In the case of further process change to the reactor 2 such as steam generation by indirect preheating). In either case, air is used as the combustion support gas a or d, and (residual) gas is used as fuel. The specified value should be understood as an approximation and any rounding error is ignored. The heating output of the combustion exhaust gas c and the heating output of the cooling combustion exhaust gas g correspond to sensible heat, and the heating output of the pressurized steam f corresponds to the sum of sensible heat and evaporation enthalpy.

  Tables 6A through 6C below represent comparable ways of illustrating the advantages of the present invention over each other. In all tables, the same amount of current ("Current Generation" column in the table) should be generated in the facility as a whole, and the same amount of reaction product (in this case hydrocarbon ethylene, " “Ethylene production” column) is produced in the reactor 2. Reference should be made explicitly to the above description of the drawings, in particular to the introductory paragraph of the drawing description.

  Assume further that the current is generated by pressurized steam f. This mainly serves to improve the comparability of the methods in terms of electrical efficiency and “efficiency” in the sense of the above definition. Thus, the “current generation” column in the table, or the value shown therein, assumes a typical electrical efficiency of 0.24 for pressurized steam f at 520 ° C. and 120 bar, and pressurized steam f It also includes currents generated from

  Row 1 of the table (“Reactor, power supply current”) contains the value of the current supplied by the power supply and the value of the reactor 2 operating in a self-sustaining manner according to FIG. An efficiency of 0.33 is assumed for the generation of current supplied from the power source. This value corresponds to a typical rating of current from a conventional power source (ie, the average electrical efficiency on the power plant network by the supplier, which includes all types of old and new Power stations, including pure (coal) steam power stations and gas and steam power stations, including all wire losses). Thus, current is supplied from the power supply according to row 1 if it is not generated from pressurized steam f.

  The ignition output corresponding to the efficiency level of 0.33 required to generate this percentage of current supplied by the power source is included in the total heating output required ("Total heating output" column in the table), The total heating power is required in addition to the heating power of the reactor 2 to make the methods comparable. This heating output is further shown as a heating output normalized to the heating output ("heating output%" column in the table).

  Row 2 of the table (“Reactor, Gas / Steam Power Plant”), as already specified in Row 1 of the table, for example, individual gas / steam power plant according to FIG. This results in a combination value with reactor 2. The heating power required to generate the current in the gas-power plant depends on the overall electrical efficiency, which is assumed here to be 0.56 (see note on Fig. 1), the total heating power mentioned in the above table column (In addition to the heating power of reactor 2).

  Looking at rows 1 and 2 together, the same power generation (current generation in the table), including the current obtained from the power source (row 1 in the table) or the current generated at the gas and steam power plant (row 2 in the table) Column), and for the same production amount of reaction product ethylene, the reduction in required heating power is due to different electrical efficiencies (overall electric efficiency of 0.56 for current generation in gas and steam power plants, comment on Figure 1). (See reference; 0.33 for typical power supply current, see above) indicates that it can be achieved immediately according to row 2 of the table.

  The specific energy consumption of the process based on the same amount of reaction product ethylene ("Specific energy consumption" column in the table) is reduced accordingly, and thus the process in the sense described above in this specification. The “energy efficiency” increases accordingly. The efficiency level associated with reactor 2 does not change because reactor 2 continues to operate satisfactorily in self-sustaining operation.

  In Table 6A, the values in rows 1 and 2 of the table described above are related to the complex facility 400 according to FIG. 3, assuming that the total current generation is 152 MW in row 3 (“complex facility 400 according to FIG. 3”). Compare with the value you want. According to row 3 of the table, out of 152 MW, 118 MW is generated by the gas turbine 1 and 34 MW is generated from the pressurized steam f with a corresponding (low) efficiency (this simplification is a comparison The actual use of pressurized steam f is typically used to drive the compressor or pump directly using shaft power, in either case typically the generator Apart from 1% marginal loss, it corresponds to electricity).

  Due to the radiation zone efficiency degraded from about 0.42 to about 0.37, in this case, increased heating power must be used in the reactor 2 for the same amount of reaction product. For this reason, the heating power according to table column 3 is 1,270 MW overall, which is clearly not only a 0.1% marginal improvement for table column 2 but also a significant improvement for table column 1 Also represents improvements.

  The fuel consumption to generate electrical energy is determined in two reference cases according to columns 1 and 2 (ie, separate generation of current and reaction products and generation by stand-alone operation) with respect to the power possible for combined generation. (Thus, the reference case is “adapted” with the knowledge that gas and steam power plants with less than 80 MW power are unlikely to be installed as independent power plants. This also applies to the table below. Heating power and specific energy consumption are interrelated with each other because the heating requirements constitute significantly more than half of the total energy consumption.

  In Table 6B, columns 1 and 2 of the table already described in connection with Table 6A and having the same meaning as Table 6A are shown in column 3 (“combined facility according to FIG. 5”) in the combined facility 200 according to FIG. The relevant values are compared assuming a current generation value of 108 MW. This value is the current generation value of the gas turbine 1 when the steam generation value in the reactor 2 is the same as the steam generation value in the self-operating reactor.

  For the dispersion of the combustion exhaust gas c in the partial streams c ′ and c ″ and for the partial use used only for preheating in the preheating device 4 and for the partial feed into the reactor 2 of the combined installation 200 according to FIG. The radiation area efficiency can be kept constant compared to columns 1 and 2 of the table, i.e., at the value of about 0.42 described above. Thus, for a given combination of parameters, the required heating power is significantly reduced, i.e. about 6% compared to Table Column 2 and about 17% compared to Table Column 1. The specific energy consumption is based on the same amount of reaction product ethylene and decreases significantly accordingly. At the same time, as already mentioned, the corresponding reactor 2 can continue to operate under conventional conditions.

  In Table 6C, the values in columns 1 and 2 of the table are compared with the values associated with the complex facility 100 according to FIG. 4 in column 3 (“composite device according to FIG. 4, 498 ° C.”). Assuming 498 ° C., ie preheating according to Table 4B, the current generation by the gas turbine is 60 MW. Of these 60 MW, 43 MW should be removed (row in the table “reduced steam generation as power”). This is because less steam is produced and the corresponding lack of shaft power is simply compensated by power. A loss of typically about 3% for the electric engine used is ignored for simplicity.

  Current generation is identical when compared to columns 1 and 2 of the table, while there is another significant drop in heating power, again due to radiation zone efficiency increasing dramatically to a value of about 0.53. .

  The combined study in the table above is particularly carried out using fuel (for example, reactor 2), partial generation with residual gas from the corresponding method, using a typical power plant mix. , Or compared to current generation by acquisition from a power source, whether using a gas / steam power plant according to FIG. 1 or a known combination of the form of equipment 400 according to FIG. To achieve an increase in A prerequisite here is in particular the sufficient availability of, for example, a suitable residual gas. Furthermore, it can be seen that the known combination of the form of the installation 400 according to FIG. 3 has little or no efficiency advantage over the individual production of current and reaction products, ie, in the example shown above, the same Requires heating power and thus comparable fuel supply.

  The proposed installation 200 according to an embodiment of the present invention has an efficiency of about 6% higher when compared with individual current generation by gas and steam power plants and individual production of reaction products in the self-sustaining reactor 2. When comparing the acquisition of current from a typical power plant mix, or power supply, with the individual production of reaction products in the stand-alone reactor 2, an increase in efficiency of about 11% is observed.

  The facility 200 produces 92% current for an additional unit of ignition power used (ie, 0.92 MW for 1 MW of used heating power in addition to the heating power required for operation of a stand-alone reactor). To generate). This value corresponds to approximately twice the electrical efficiency of the gas / power plant, or three times the electrical efficiency of obtaining current from the power plant mix or power source.

  The proposed facility 100 requires less heating power than a self-sustaining reactor and generates additional current. Thus, the installation 100 has an efficiency of about 11% higher when compared to individual current generation by gas and steam power plants and individual production of reaction products in the self-sustaining reactor 2.

Claims (15)

  A method for combined production of mechanical power and production of hydrocarbons, wherein combustion exhaust gas (c) is generated by igniting at least one internal combustion engine (1) to generate said mechanical power, A method of heating at least one reactor (2) using fuel (e) and combustion support gas (d) to produce hydrocarbons, wherein at least a portion of said combustion support gas (d) comprises: Heating by indirect heat exchange with at least a portion of the combustion exhaust gas (c) from the internal combustion engine (1).   The method according to claim 1, wherein the mechanical power is at least partly converted into electric power by at least one generator (G) and / or used to drive at least one shaft.   The method according to claim 1 or 2, wherein the at least one reactor (2) is configured as a tubular reactor, and in the radiation zone the reaction tube is heated from the outside by a burner that burns the fuel.   The process according to claim 3, wherein the feed stream is passed by pressurized steam through the reaction tube of the reactor (2) configured as a tubular reactor to produce the hydrocarbon.   The process according to claim 3 or 4, wherein the catalyst is fed into the reaction tube of the reactor (2) configured as a tubular reactor.   The process according to any one of the preceding claims, wherein the fuel (e) is produced at least in part from a gas mixture separated from the product stream from the at least one reactor (2). .   At least one region of the at least one reactor (2) is within the at least one region of the at least one reactor (2) by the use of the fuel (e) and the combustion support gas (d). 7. A method according to any one of claims 1 to 6, wherein the heating is carried out to a temperature level of 1500 to 2500 ° C, in particular to a temperature level of 1500 to 2500 ° C.   The method according to any one of the preceding claims, wherein the at least one internal combustion engine (1) comprises at least one gas turbine.   The combustion exhaust gas (c) from the internal combustion engine (1) is supplied at a temperature level of 500 to 1,000 ° C, in particular at a temperature level of 600 to 700 ° C, or a temperature level of 500 to 650 ° C. Item 9. The method according to any one of Items 1 to 8.   A portion of the combustion exhaust gas (c) from the internal combustion engine (1) is used to heat the combustion support gas (d) by indirect heat exchange and the combustion from the internal combustion engine (1). A portion of the exhaust gas (c) is mixed with the combustion support gas (d) and fed to the at least one reactor (2) together with the combustion support gas (d). The method according to any one of the above.   In order to heat the combustion support gas (d) by indirect heat exchange, the combustion exhaust gas (c) from the internal combustion engine (1) is entirely used, and the at least one reactor (2) is used. 10. The method according to any one of claims 1 to 9, wherein no supply is provided.   Natural gas and / or methane-containing gas mixture, in particular a gas mixture containing hydrogen, methane and carbon monoxide produced according to claim 6 is used as the fuel (e) and / or air is used as the combustion aid. 12. The method according to any one of claims 1 to 11, wherein the method is used as a gas (d).   Pressurized steam (f) is generated from waste heat from the at least one reactor (2) and is used in particular for driving at least one shaft of the generator (G). The method as described in any one of these.   An installation (100, 200) for combined generation of mechanical power and hydrocarbons, the installation (100, 200) comprising at least one internal combustion engine (1) for generation of the mechanical power; and Comprising at least one reactor (2) for the production of said hydrocarbons, said at least one internal combustion engine (1) being capable of producing combustion exhaust gas (c) by ignition, said at least one reaction The vessel (2) can be heated using the fuel (e) and the combustion assist gas (d) in the facility (100, 200), the combustion exhaust gas (c) from the internal combustion engine (1) An installation (100, 200) characterized in that it provides means to heat at least a portion of the combustion assisting gas (d) by indirect heat exchange with at least a portion of the combustion assist gas (d).   15. Equipment (100, 200) according to claim 14, arranged to carry out the method according to any one of claims 1 to 13.

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